Apparatus for conducting catalytic reactions



April 17, 1945.

K. H. HACHMUTH APPARATUS FOR CONDUC'IIING CATALYTIC REACTIONS original Filed May '7, A1940 ldeposited on it during use.

Patented Apr. 17, 1945.

, APPARATUS FOR CONDUCTING CATALYTIC v REACTIONS Karl H. Hachmuth, Bartlesville, Okla., assignor to Phillips Petroleum Company, a corporation of Delaware Originall application May 7, 1940, Serial No. 333,872. Divided and thisapplication March 10, 1942, Serial No. 434,126

12 Claims.

This invention relates to the conducting of catalytic reactions and more particularly to the conducting of a catalytic reaction within an elei any further increase in temperature `is unprotable or is otherwisel undesirable: At this point the catalyst is replaced, or lit is revivied by a procedure that removes the deactivating material When only one portion of catalyst is used at a time, the replacement or the revivilcation causes an undesirable interruption of the catalytic reaction; -for this reason,

two or more portions of catalysts, generally within individual catalyst chambers, are preferably used. These portions become fully deactivated one by one in turn, at approximately equal intervals of time, and each is replaced by fresh or ,revivied catalyst without interrupting the conversion occurring in the other portions. During use of such a multiplicity of portions of catalyst,

the catalytic reaction or conversion must be effected at different temperatures in the various, portions, in accordance with the different de7" grees of catalytic activity, in order that each portion may effect its share vof the aggregate conversion.

In the past, the different temperatures required vin the various portions of catalyst have been obtained by s-eparately heating each portion or body of catalyst, or 'the stream of reactant material coming into contact therewith, to the proper temperature; this systemY entails the use of a separate heating unit for each portion of catalyst. and

, each unit must be continuously adjusted to procomplexity both in the amount of the heating equipment and in its operation.

In one modification, the present invention comprises the steps of dividing a stream of material, which is to undergo a catalytic reaction, into at least two swbstreams; heating one of the substreams to at least about the maximum temperatureat which the reaction' is to be effected, any effect of the reaction itself upon the temperature being disregarded, or to about the maximum temperature desired for the charge stock for the re,- action; and forming from the hot substream and the cooler substream a multiplicity of reactant streams equal in number to a multiplicity of portions or bodies of a catalyst that are used simultaneously in separate catalyst zones for effecting sai-d catalytic reaction, each of said reactant streams being formed of such proportions of the heated and the unheated substreams that the temperature of the resultant stream corresponds to the instantaneous degree of activity of the body of catalyst with which itis to bein contact, in such a way .that each of the reactant streams undergoes a predetermined degree of conversion during its period of contact with the catalyst.

One of the objects of the invention is to provide a process of obtaining different reaction temperatures in two or more separate catalytic reaction zones, arranged in parallel and provided with portions of catalyst or -With different catalysts for the same reaction, that differ in activity, in such a manner that each zoiieior portion effects a predetermined share of the aggregate conversion.

, Another object is to electby means of a single heating unit, the establishment of different temperatures in two or more parallel streams of reactant material that subsequently pass into contact with separate portions of a catalyst that have diffrent instantaneous degrees of catalytic activityl.

Still another object of the invention is to use a single heating unit to provide v,a heat-carrying material to two or more reaction zones which are maintained at different temperatures.

A further object of my invention is to obtain, v

from a single charge stream and a single heating unit, two or more charge streams of diierent v and independently variable temperatures.

streams to form a composite stream with desired characteristics.

Other objects and advantages of the invention will be obvious to those skilled in the art.

The invention may be used for the conduction of any process which involves a catalytic reaction that requires a temperature differing from atmospheric temperature and it may be used in connection with either an endothermic or an exothermic reaction. Although the invention will generally be practiced in connection with reactions at elevated temperatures, it may be readily applied to reactions carried out/'at low temperatures by cooling one of the substreams.l It is especially valuable for conducting catalytic reactions involving hydrocarbons either as reactants or as products, such as hydrogenation, dehydrogenation, polymerization, depolymerization, alkylation, cracking. desulfurization, oxidation, hydration, dehydration (such as of alcohols to olens), and the like; but it may be used also for conducting catalytic reactions in which hydrocarbons are not involved.

Numerous methods may be employed for blending portions of the hot and of cooler substreams to form a charge stream having a desired temperature for any particular catalyst chamber. In a modiiication which may be often used,

branch pipes, each controlled by an individual c be varied as to temperature without appreciable variation in total volume, when a substantially constant total volume is to be used. However, I have found that flow control valves do not generally operate entirely trouble-free on hot streams, and have developed other and novel means for controlling the streams. In such a novel modification, the rate of flow of the composite stream is controlled or limited by suitable ow control means, or is maintained at the maximum capacity of the pipe or conduit through which it ows, and a now-control valve on the cooler stream is actuated by a temperature responsive device, no control valve being used on the hot stream, The flow of the hot stream is thus controlled indirectly, without the direct use of a separate valvey by the cooperation of the actions of the limitation of flow of the composite stream and the flow control of the cooler stream.

Solely for the sake of simplicity, it being understood that the invention is not to be limited thereby, an application of my invention will be described in connection with the conduction of the polymerization and olens at elevated temperatures, such as the polymerization of normally gaseous olens to gasoline-range hydrocarbons.

The accompanying drawing is a flow-diagram illustrating diagrammatically a specific embodiment of the invention as applied to such a polymerization. Substantially the same arrangement can be used in a dehydrogenation process, or the like.

The feed, comprising polymerizable oleflns, en-

` ters the system through inlet I and pump 2, which maintains it at any desired pressure. It is divided into two substreams, one of which is heated to a desired temperature in heating coil 3 in heater 4, and the other of which passes unheated, or only partially heated, through conduit 5. The

temperature to which the first substream is heated generally is at least as high as the maximum temperature desired for the charge stock to the polymerization step in the presence of the least.

active catalyst body that is to be used in the subsequent polymerization chambers; in addition, the temperature should be high enough to compensate for any heat loss occurring prior to the polymerization. A temperature of about 450 to 600 F. is suitable for most purposes, but it may be higher or lower than this value in particular instances. The temperature is preferably maintained at a substantially constant level by means of an automatic temperature controller, not shown, that regulates the input of heat or of fuel to heater 4.

Although generally coil 3 is so constructed that the pressure drop in it and conduit 6, taken together, is greater than that in conduit 5, at times it may be desirable to increase the resistance to fiow of the heated substream. Such an increase may be readily effected by constricting this substream, as by control-valve 3| or by a constriction in conduit 6.

The not substream passes from heater 4 through conduit and manifold 5, from which lead branch pipes 1, 8, 9, I 0, The cooler substream passes through valve 45 and conduit and'manifold'5, from which lead branch pipes II, I2, I3, and I4. Branch pipes 1, 8, 9, and I0 are joined to II, I2, I3, and I4, respectively, and from their junctures pipes I9, 20, 2|, and 22,1ead to catalyst chambers 23, 24, 25, and 26, respectively. The rates of flow through pipes I9, 20, 2|, and 22 are preferably controlled by flow-control valves 21, 28, 29, and 30, respectively, and are generally held substantially constant for long periods of time. 'I'his flow control is adapted to set a maximum on the total now, more than suicient material being available to supply this'maximum. In some instances the capacity of any one of the pipes I9 to 22 may be a sufficient limit and maximum, so that no additional control is necessary. In most cases, however, it will be desirable at times notl to reach the capacity of the pipe carrying the combined streams as a maximum and for this reason some sort of now-control, as shown, will be used. These flow-control valves vmay be manually or otherwise operated, as desired, but very satisfactory operation is obtained by having them automatically controlled through the agency of means actuated by an orifice flow meter, or other type of flow meter, represented by 21', 28', 29', and 30', respectively, and which may be on either the upstream or downstream side with respect to valves 21, 28, 29, and 3U, respectively, the former arrangement being preferred. The individual regulating means may all be set to the same flow rate, or to different flow rates, as individual circumstances may indicate is desirable or necessary. The temperatures of the composite streams owing through each of the pipes I9, 20, Aand 2I and 22 are regulated by flow-control valves I5, I6, I1, and I8 in branch pipes II, I2, I3, and I4, respectively, which convey the cooler material. These valves may be manually or otherwise operated, as desired, but I have obtained good performance by having them actuated by temperature responsive devices or means which respond to the temperatures of the composite streams in conduits I9, 20, 2|, and 22, as represented by I5', I6', I1' and I8', respectively, With this arrangement, a slight positive differential is maintained in manifold 5 over that in manifold 6, thereby insuring a positive flow through the control valves I5, I3, I1, and I8 at all times. The temperature responsive devices should be placed at a sufficient distance from the union of the hot and cooler-streams to result in accurate control,such as at a sufficient distance to insure effective mixing of the streams. Other means for accomplishing the same result may be used, but for most applications this arrangement is the simplest. A number of automatic controllers, or similar means, are available commercially, and can be readily adapted by one skilled in the art. Such may be set to any desired temperature or temperatures for the composite streams, and will then operate the flow control valves I to I8 to maintain such temperatures. Such temperature values may be changed from time to time as desired, either by hand or automatically, as referred to hereinafter.

In catalyst chambers 23, 24, 25, and 26 polymerization of oleiins to heavier hydrocarbons is effected in the presence of a polymerization catalyst. tains a different portion or body of the same catalytic material, and in general at any particular moment the different bodies of catalyst have different degrees of activity and hence require different temperatures, all other conditions being the same, to effect substantially the same prevautomatic controller` may be changed by a secondary automaticV controller that is responsive, directly or indirectly, to the extent of polymerization effected by the corresponding catalyst body;

that is, the secondary controller (illustrated as I5", I6". I1", and I8") being actuated by some characteristic of the eflluent streams in the appropriate conduit 23', 24', 25', or 26', respectively, leading from one of the catalyst chambers 23, 24, 25, or 26, and so setting or controlling the primary controller I5', I6', I1', or I8' that the temperature of the reactant stream is adjusted to that required to eiect a definite predetermined degree or extent of polymerization. For example, the secondary controller may be made responsive to the change in composition of the effluent stream that leaves the catalyst chamber, orto the change in temperature that takes place between inlet and eiliuent streams as a result of the polymerization, which is an exothermc reaction. Since sui'llcient material is available to maintain the maximum flow through any one of the' pipes I9 to 22 at all times, a decrease in the cooler stream automatically results in a rise in temperature of the composite stream without changing the total ilow rate, and the converse is also readily obtained.

Although no restriction as to the size of the various portions or bodies of catalyst, or of the tially equal in size. However, at times the reactant streams may be advantageously made different in size; thus if one or more of the catalyst bodies is different from the rest as to size, a corresponding difference may be maintained for the reactant stream, or one or more of the streams may be made relatively disproportionate to the size of the portion of catalyst with which it comes into contact if catalyst bodies of equal size are used. For example, at times improved results may be obtained with a relatively less active, or a relatively deactivated catalyst portion by a rate of flow lower than that used for the other catalyst portions. Such a relatively low rate tends to decrease the temperature required, to increase the quality of the product. and to prolong the Each catalyst chamber generally convarious reactantrstreams, is necessary for the,-

operation of the invention, it is` generally pre-` ferred to use portions of substantially equal size I period of use of the catalyst portion by decreasing its rate of deactivation. Conversely, if it is desired to hasten the deactivation of a particular catalyst portion, in order that its removal from the process upon deactivation shall occur at the predetermined time, the rate of ow may be made relatively large.

Regardless of the requirements in any particular case, the preferred arrangement of control valves shown is so flexible that they can be met, By its use, individual operation of each catalyst chamber in any desired manner can be obtained within broad limits of pressure, temperature, and rate of flow, independently of the manner of operationof the other catalyst chambers, and any chamber may be removed from the system or other chambers may be introduced as will be appreciated.

After the polymerization has been effected in catalyst chambers 23, 24, 25, and 26, the various streams of products pass through gate valves 32, 33, 34, and 35, respectively, and are combined. The resulting composite effluent stream passes through control valve 36, which serves as a pressure reduction valve, and conduit 31 to fractionator 38, in which fractionation is effected into at least two fractions, such as a fraction containing the desired polymer product, which may be withdrawn from the systemthrough valve 39 and outlet 40, and relatively light or unreacted hydrocarbons. which may be withdrawn through valve 4I and outlet 42, and which may be treated in whole or in part to increase the concentration of olens, as by dehydrogenation, and then reprocessed.

Although the substream 5 has been primarily described as an unheated stream, it may be heated t0 a certain extent, preferably not above the minimum temperature desired for any particular reactant stream. This partial heating may be accomplished by any desirable or available means, as by indirect heat exchange With the catalyst effluent or by heat exchange in the economizer section of a furnace, thereby utilizing waste heat and reducing the heat input of heater 4. In case two separate streams-are available, one may be heated as discussed and the other introduced in an unheated condition through pipe 44, with valve 45 in pipe 5 partially or completely closed, asmay be desired. In a catalytic cracking or dehydrogenation process, for example, the heated stream may comprise recycled unreactcd material while the unheated stream may comprise fresh charge stock. The hot stream may be subjected to control rather than the cooler one, although such an arrangement ordinarily will not be desirable, except with subpurpose of illustrating a few of the many possible modes of operation of the invention; they are not to be taken as establishing any limitations of the invention.

Example I A feed having the following mol-percentage composition was used as chargeV to a catalytic polymerization operation:

This feed was pumped to a pressure somewhat exceeding 1500 pounds per square inch; its temperature was about 100 F. Part of the feed stream was heated to a temperature of about 600'Jv F. in a tube coil heated by the burning of fuel gas. Thetemperature of the heated stream was maintained substantially constant by an automatic controller that regulated the amount of fuel gas being burned. Passage of this part of the feed stream through the tube coil caused its pressure to decrease to about 1500 pounds per square inch. The other part of the feed stream was not heated.

Four catalyst chambers of equal size were used, all containingsubstantially equal amounts of a solid, granular silica-alumina polymerization catalyst comprising alumina absorbed on silica gel similar to that described in McKinney, Patent No. 2,142,324. However, only three of the chambers were used at a time, the fourth being ready to be used in its turn upon deactivation of one of the three. That is., the fourth chamber was conditioned for use during operation of the other three, as by revivication of spent catalyst or by replacement of spent catalyst with fresh catalyst, and was put into operation when a chamber containing deactivated catalyst was Ethylene 0.60 Ethane 0.35 Propylene 5.53 Propane 8.11 Butylenes 1.63 Butanes 83.78

The extent of polymerization was 18.8 per- -cent by weight of the feed. As each catalyst body underwent progressive deactivation, the temperature had to be correspondingly increased, in order for the extent of polymerization to be maintained. Finally, when the temperature of the incoming reactant stream reached 450 F., the body of catalyst was considered sufficiently deactivated to be removed from service and replaced by a fresh or a revivied body of catalyst. The catalyst used was capable of polymerizing at a satisfactory rate up to a temperature of about 600 F., but the proportion of polymers heavier than the dimer in the product vtended to increase at temperatures above about 450 F., which was undesirable for the present operation.

The catalyst chambers were not heated otherwise than by the reactant streams. The chambers were insulated against excessive heat loss; what heat loss occurred was more than compensated by exorthermic heat of polymerization, which in addition caused the temperature of the eiuent to be about 30 to 90 F. above that of the incoming reactant stream.

Each of the three reactant streams going into the three catalyst chambers in simultaneous use was formed from both the feed stream heated to about 600 F. and the unheated feed stream at about F. An automatic controller, actuated by a thermocouple located in the reactant stream at the inlet of the catalyst chamber, adjusted a valve controlling the addition of the unheated material to the heated material going to the chamber; that is, this controller so increased or decreased the cold feed to the chamber that the temperature of the composite, rea-etantl stream was substantially constant at the value necessary at the moment for the desired extent of polymerization to be effected. From time to time, as the catalyst progressively became deactivated, the setting lof the controller was manually changed, so that the temperature of the reacting stream was correspondingly increased and the extent of polymerization was maintained at substantially the same level until finally the body of catalyst was so deactivated as to require replacement or revivification.

An automatic ow controller, actuated by an orifice flow meter through which the reactant stream passed just before reaching the catalyst chamber, controlled the rate of iiow of the composite reactant stream by automatically adjusting'a flow-control valve, through which the composite reactant stream passed, in such a way as to compensate for fluctuations in the pressure and in the back pressure developed in the catalyst chamber.

The extent of polymerization in each individual catalyst chamber was followed by weathering 10G-cc. samples of the effluent, withdrawn from the outlet of the chamber through a small cooling coil immersed in an ice bath. After the weathering, which took place at atmospheric pressure. the amount of residue remaining at 100 F. indicated qualitatively the extent of polymerization, and`the temperatures in the individual chambers were adjusted until all gave the same amount of residue. Periodic determinations of `the butylene content of the eiiiuent indicated quantitatively the thoroughness of the polymerization. If too much butylene was present in the eliluent, the temperatures in all three chambers were increased; later, small adjustments were made individually to bring the chambers back A -cipally heptenes and octenes, kbefore the inlet temperature reached 450 F.

Ervample II In another polymerization process a total of five Icatalyst chambers were used, four being onstream at a time. The unheated feed stream was at a pressure of about 1540 pounds per square inch and a temperature of about 100 F.; the heated feed stream was at a, pressure of about 1500 pounds per square inch and a temperature of about 500 F. As in Example I, a, granular silica-alumina catalyst was used. The change effected by the polymerization is indicated by the following composition of the feed stream and yof the effluent fromv the catalyst chambers, in percentages by weight: y

In this sample, the temperature and thev rate of iiow of each of the four reactant streams were controlled and adjusted substantially in the mani ner described in Example I.

Although in the foregoing two examples the degrees of activity, and the use of different temperatures obtained in the manner described, results in an evening-out of the heat load on the fractionating system that fractionates the eiliuent from the catalyst chambers. This advantage becomes the greater, the larger the number of catalyst chambers; for, with an increase in this num` ber, the disturbance in heat load resulting from the replacement of a spent portion of catalystI by a fresh portion becomes relatively smaller. However; a number within the range of three to six is usually adequate, and'therefore such a number is preferred.

Many modifications and variations of this invention may obviouslybe used, and can be adapted by one skilled in the art without departing from the spiritof the disclosure. The restrictions used and conditions have been described and the modications discussed in suiiicient detail to serve' as eicient guides. Although catalytic cracking and dehydrogenation operations are endothermic rather than exothermic, the fundamentals of my invention may be applied to such processes with success, with suitable allowances for known differencesy between exothermic and endothermic processes.r

This application is a division of my copending application Serial Number 333,872, filed May 7, 1940. l i

I claim: f l

1. In combinatio a plurality of catalytic reaction chambers, conduits for conducting a stream of reactants to each ,of said chambers, conduits for conducting a stream of hot reactants to each of said first named conduits, conduits for conducting a stream of relatively cooler reactants to each of said rst named conduits, ow control means in each of said last named conduits, and temperature responsive means in each of said first named'conduitsF operatively associated. with said iiow control means in the corresponding one of said last named conduits to vary the now in each of the cool reactant conduits in response to temperature variations in the stream in the corresponding first named conduit.

2. A combination as defined in claim 1 in which means are provided for limiting Athe maximum flow rate in each of said first named conduits.

3. In an apparatus for conducting catalytic hydrocarbon conversions, in combination, a plurality of catalyst chambers arranged in parallel, conduit means for bringing a main stream of hydrocarbon to be connected into the system, juncture means f or splitting said main stream into two substreams, single heating means for heating one of said substreams to at least the maximum temperature to be employed for the feed to any of said chambers, first conduit and manifold means for conveying said heated substream from said in the examples, and in connection with the drawing, need not necessarily be used as limits for all particular koperations or sets of conditions, since they are presented primarily as illustrative examples. It will be understood that the now diagram presented and described as a part of the disclosure is schematic only, and that many additional conventional pieces of equipment, such as pressure gauges, valves, pumps, heat exchangers, reux lines and accumulators, heaters and coolers, and the like, will be necessary for any particular installation, and can be supplied to meet the requirements of any particular caseby anyone skilled in the art. The essential equipment heating means towards said chambers, second conduit and manifold means for conveying the other substream from said juncture means towards said chambers in substantially unheated condition, a plurality ofrst conduits for conveying from said first manifold means towards said chambers a corresponding number of parallel heated streams, an equal number of second conduits for conveying from said second manifold means to juncture with said first conduits an equal number of parallel substantially unheated streams, third-conduits for conveying the merged streams in parallel from said junctures into said chambers, valve means in said second conduits for controlling the iiow of the streams therein,

and means responsive to the temperatures of the respective merged streams in said third conduits for automatically controlling said valve means and thereby individually and independently controlling the temperatures of the respective merged streams fed to each of said chambers.

4. An apparatus as dened in claim 3 wherein said first conduits are unvalved and free from obstruction. f

5. An apparatus as defined in claim 3 wherein said third conduits contain flow valves and means responsive to the rate of ow in said third conconduits form a straight conduit unvalved and free from obstruction.

'7. An'apparatus as defined in claim 3 wherein said manifold means supply sufficient material to meet the maximum flow limit of said third conduit means.

8. An apparatus as defined in claim 3 wherein means is provided for maintaining a positive pressure differential in said second manifold means over the pressure in said first manifold means for thereby insuring a positive fiow through said second conduit means at all times when said valved means allows flow therethrough.

9. In an apparatus for conducting catalytic hydrocarbon conversions, in combination, a plurality of catalyst chambers arranged in parallel,

conduit means for bringing a main stream of hydrocarbon to be connected into the system, juncture means for splitting said main stream into two substreams, single heating means for heating one of said substreams to at least the maximum temperature to be employed for the feed to any of said chambers, first conduit and manifold means for conveying said heated substream from said heating means towards said chambers, second conduit and manifold means for conveying the other substream from said juncture means towards said chambers in substantially unheated condition, a plurality of first conduits for conveying from said first manifold means towards said chambers a corresponding number of parallel heated streams, an equal number of second conduits for conveying from said second manifold means to juncture with said first conduits an equal number of parallel substantially unheated streams, third conduits for conveying the merged streams in parallel from said j unctures into said chambers, fourth conduits for conveying the products from the catalytic chambers, valve means in vsaid second conduits for controlling the flow of the streams therein, and primary means responsive to the temperatures of the merged streams in said third conduits and secondary means responsive to the temperatures of the product streams from the respective catalytic chambers, said primary and secondary temperature responsive means automatically and cooperatively controlling said Va1 ve meansand thereby individually and independently controlling the temperatures of the respective merged streams fed to each of said chambers.

l0. In combination, a plurality of catalytic reaction chambers, a charge conduit for each of said reaction chambers for conducting a Vstream of reactants to said chambers, a charge manifold for relativel7 hot reactants, a charge manifold for relatively cold reactants, unvalved branch conduits connecting said hot reactant manifold and each of said charge conduits, branch conduits connecting said cold reactant manifold and each of said charge conduits, iiow control valves in each of said last-named branch conduits, a common charge conduit connecting through a juncture with conduits to both the aforesaid hot and cold reactant manifolds for conducting a common reactant to both said reactant manifolds, heating means on the conduit connecting the last-named common charge conduit with the hot reactant manifold for heating the reactant stream passing through said conduit to the hot reactant manifold, a discharge manifold, and a discharge conduit connecting each of said reaction chambers and said discharge manifold, wherein the flow-control valves in each of the branch conduits connecting the cold reactant manifold and the respective charge conduit are operatively associated with means responsive to temperatures of reactants entering the respective catalytic reaction chamber.

- 11. In combination, a plurality of catalyticreaction chambers, a charge conduit for each of said reaction chambers for conducting a stream of reactants to said chambers, a charge manifold for` relatively hot reactants, a charge manifold for relatively cold reactants, unvalved branch conduits connecting said `hot reactant manifold and each of said charge conduits, branch conduits connecting said cold reactant manifoldand each of said charge conduits, flow control valves in each of said last-namedbranch conduits, a common charge conduit connecting through a juncture with conduits to both the aforesaid hot the respective charge conduit are operatively associated with primary means responsive to temperature of reactants entering the respective catalytic reaction chamber and with secondary means responsive to changes of composition of the products'leaving the respective catalytic reaction chamber.

12. In combination, a plurality of catalytic reaction chambers, a charge conduit for each of said reaction chambers for conducting a stream of reactants to said chambers, a-charge manifold for relatively- Vhot reactants, a charge manifold for relatively cold reactants, unvalved branch conduits connecting said hot reactant manifold and each of said charge conduits, branch conduits connecting said cold reactant manifold and each of said charge conduits, flow control valves in each of said last-named branch conduits, a common charge conduit connecting through a juncture with conduits to both the aforesaid hot and cold reactant manifolds for conducting a common reactant to both said reactant manifolds, heating means on the conduit connecting the last-named common charge conduit with the hot( reactant manifold for heating the reactant stream passing through said'conduit to the hot reactant manifold, a discharge manifold, and a discharge conduit connecting each of said reaction chambers and said discharge manifold, wherein the. flow-control valves in each of the branch conduits connecting the cold reactant manifold and the respective charge conduit are operatively associated with primary means'responsive to temperature of reactants entering the respective catalytic reaction chamber and secondary means responsive to temperature of the products leaving the catalytic reaction chamber.

KARL H. HACHMUTH. 

